Process for catalytically convert



July 18, 1950 w. J. DEGNEN PRocEss FoR CATALYTICALLY coNvERTNG HYDROCARBON OILS 5 Sheets-Sheet l Original Filed Jan. 28, 1941 BYCc/g: i( t ATTORNEYS July 18, 1950 w. J. DEGNEN PROCESS FOR CATALYTICALLY CONVERTING HYDRocARBoN ons 5 Sheets-Sheet 2 Original Filed Jan. 28, 1941 July 18, 1950 w. J. DEGNEN 2,515,369

v PROCESS FOR CATALYTICALLY CONVERTING HYDRocARBoN ons Original Filed Jan. 28, 1941 3 Sheets-Sheet 3 :Nvt-:mn WILL/M I DEG/VEN BY g, 5', JM

ing; the-.conversion period.

Patented July 18, 1950 PROCESS FOR CATALYTI'CALLY CONVERT- ING HYDROCARBON OILS William J. Dog-nen, Westfield, N. J., assigner to- The M. W. Kellogg Company, Jersey City, N.` J a corporation of Delawarev Original application January 2E; 1941, Serial No.

Divided and this.- application. .August 31, 1946,. Serial No. 694,342

5 Claims. (Cl. 19.6-152) y Myv invention relates to process and apparatus for converting hydrocarbonsy in the presence of a catalytic: material.. The art of cracking in the presence: et a catalyst is-rwe1l known where the catelystvismaintained ina bed and the liquid or vapor tovbe treated is passed through the bed dur- Tov regenerate or revivifyv a bed. oi catalyst in situ, it is necessary to Subject the catalytic material to heating in such manner aS,- to burn off. carbonaceous or contarxxinatinu;A materials and. diiliculties have continually arisen intharegeneration of the catalyst.

More 'particularlyY it has been. proposed heretofore to: eatalyttcally convert high boiling hydrocarbone such. as gas oil. toV low boiling hydrocarbona such as gasoline by passing vapors of the hishboil-ing hydrocarbons` under suitable reaction; conditions incontaet withz a bed. of cracking catalyst disposed in a catalyst chamber. After tht: activity of the catalyst is decreased by reasenior the formation ot a carbonaceous deposit thereon. to aA degree where regeneration is necessary or desire-bla. the activityof the catalyst` is restored by shutting ofi the flow of oil vapor to the chamber :and passing an oxygen-containing gas into the chamber in contact with the catalyst-thereby regeneratingv the catalyst in situ by combustion of the@ carbonaceousy deposit. This procedure while. constituting a practicalA commerciali operation has a number of disadvantages which;- are` eliminated by the process provided by my invention. these disadvantages are the intermittent operation, variations in product duality and quantity during the` reaction period, and difficulties in temperature control, particuiarly in. the regeneration operationU It has-been: further proposed in U. S. Patent No'.. 2,35ogl30, in which applicant is a. co-inventor, to' secure continuous operation by maintaining a bed of. granular catalytic cracking material in the reaction chamberand to maintain. the average catalyticv activity' of the bedy substantially constant throughout the operation. by adding active catalyst thereto and: removing spent catalyst therefrom by mechanical feeding means without interruption of the flow of oil vapors through the chambers. The present process has certain features in common with and alsok advantages over the process described in said patent and accordi'nglyl it may be classified. as an improvement thereover.

An object and an advantage of the present invention is to. provide a' method of converting hydrocarbons@ in the presence of a catalyst so that during the reaction time; or during the period in which the hydrocarbons are in contact with the catalytic material, temperatures of reaction can be more accurately controlled. Another object of. the inventionk is to provide an intimate mixturev or association ofv the catalytic material and hydrocarbon vapors in such manner that the vapors are aorded an opportunity for morey in.- timate mixture with the catalyst due to.. the fact lthat the'catalyst is carried along. in intimate mixture in the vapor during the reaction period.

f The method also provides a more complete and effective utilization of the catalyst and. provide a simpliiied method for regenerating or revivify-ing thelcatfalyst.

`Iri the accompanying drawings, whichform part of the specification and are to be read in conjunction therewith,

Fig. 1 is a diagrammatic showing of an apparatus inwhich the process may be operated;

Figr 2. is a modied type of apparatus using a different.- type of reactor, and reviviiier;`

Fig.. 3 is a longitudinal sectional view of suitable means for introducing a mixture of oil vapor and catalyst in the system;

Fig. 41 is a; sectional view along. the line 4-4 of Fig. 3`;V and i p Fga illustrates. a modiied type of means for introducing a4 mixture of oil. vapor and catalyst into the system.

n Reierring to the drawingsand describing the method as applied tothe cracking of topped crude in. the. apparatus,..the charge is supplied yfrom any suitable source through line I and is pumped by means of a pump. 2 through a line 3 and heat exchanger 4 to the heating coil 5 in a furnace 6. In the turnace the` charge is. heated to a. Vaporizingtemperature from 800 to 875 F. and is discharged through a transfer line 'I to an evaporater B, where the unvaporized oil is separated from .the vapor. The. tar, or unvaporized: liquid is withdrawn from the evaporator through a pipe a and is. pumped by pump I0 through a cooler IVI lto storage through the pipe I2, or may be recirculated through line I3 to the transfer line 'l landback intothe evaporator. Valves in the lines I2; and I3.4 furnish means for controllingv this ow as described.. The vapors rise in the evaporator and are directed through the vapor line I5 to heating coil i6- positioned in furnace I1, where theavapor temperature: is raised. to a suitable conversion temperature, preferably 925 F.. asv a maximum. Into the top of the evaporator may bei introduced a cooling liquid through the pipe I 8- info-rder toregulate the top temperature mai-ntained in the evaporating stage. From the vapor pulverulent form, such that it may be readilyk carried along with the vapor through the reaction zone. The catalytic material is supplied lfrom any convenient source, through a hopper 25 controlled by a valve 26 into a hopper 21, whose discharge is connected to the solids-pump 23, and is panyjand iswdescribedin detailin U. S. Patent No1. 1,553,539, `and a modication thereof in U. S.

PatentNoi2,102,330.y A similar commercial device is known as the Airveyor, the difference between the Airveyor and the devices shown in the patents referred to being in the relative amount of carrier or gas used to support or carry the solid particles through the reaction zone. In the Air- 'veyor device, considerably more air or other `car' rier is used to' suspend the solid particles than is employed in the devices of Kinyon and Newvcomergdescribed in the patents. typical type of Kinyon solids-pump is illustrated in `Figs. 3 and 4. Numeral |20 indicates a cylindrical casing provided at one end with' a supporting foot |2| and connected at the other end to a standard |22, having a cylindrica1bore of the same diameter as the interior of 'the casing. Above the bore is a hopper |23 of'a suitable shape and capacity into which the catalytic material is discharged by rotary valve 28. Extending through the casing |2| and the bore of the standard |22 'is a screw element |2-5,-the shaft |26 of which projects through a suitable bushing |21 which `also serves as a closure for the outer end of the bore. The shaft is rotated by any suitable means (not shown) such as an electric motor.

IAs shown, the pitch of the screw element |25 decreases from the end at which catalytic material is supplied tothe end from which it is discharged. The purpose of this arrangement is to compress the material' as it approaches the discharge end of the screw, so that the material will `act as a seal to prevent the gas which is introduced into the material as it leaves the screw from flowing through the casin'g'toward the hopper and aerating the material before it has been discharged from the screw.

" For the purpose of introducing uid into the material `there is attached to the forward end of casing |20 an annular casting |3|, the lower portion of which is provided with a semi-circular passage |32 as shown `'most clearly in Fig. 4. This passage is substantially concentric with the bore of the casting andits ends are brought out to the exterior of the casting, preferably at dia,- metrically opposite points. One end of the passagemay: be closed by a. screw plug |33, while the other end is connected to line 22. i

For the purpose of introducing the vapor from fthe passage |32` into .the pulverized material. there isprovided a seriesof forwardly directed ports |40 `between the passage |32 and the interior. of .the casting. vThe ports |40are notlimited .to fthe, .particular number orY arrangement 4 shown, and may extend over a greater or lesser arc, and in fact may be arranged around the entire circle, in which case the passage |32 will surround the bore of the casting. The ports |40 may be locatedgat a .distance from. the end of the screw element deter-mined with reference to certain other features of the installation. As the pressure in the system against which the material is to be discharged increases there should be a greater packing'or vsealing effect behind the jets in order that the higher pressure fluid which is necessary for such increased distances should be forced into thematerial and prevented from nowing through the screw conveyor toward the hopper. This result may be obtained by locating the ports at a greater distance from the end of the Attached to the front face of annular casting |`2| is a tapering casingjor chamber |4|, the outer end of which is connected to reactor transfer line |42. MV' "'f i One of the advantages of a solids-pump' of the type illustrated is that finely divided solid mate rial after being brought. intc}sufllciently V`fluent condition may be forcedor-pumped through pipes by mechanical means in muchthe same way as waterfoils,` orother liquids `are conveyed. 9 This may -be accomplished by injectingfthe fluid into the solid material within the conveying device vin an amountwhichwill suilicet'o'- prevent packing of the material andrender it suflicientlyfluent-so that it may be propelled vthroughout-a system of considerable length bypressure 1 applied to vthe material at'one end of' the system.- The injec# tion of' the gas into the material gives ita sluggishly fluent condition which makes it possible to effect the movement of the material as described. This' condition of the mixture'- is quite "distinct from those systems'in which'fthe'particles of material are held in suspension in a relatively large volume of moving fluid. -"A`ccordingly, solidspumps of this type have the advantage of extreme flexibility with respecty tothe fproportlonsof cat= alyst and oil fed to the system;A t' vr;

To the solids-pump 23'are vsupplied .catalyst from theho'pper 21" and vapors through'the line 22.l The vaporsare at a suitablereaction-.Jtem perature and are mixed with the catalystto form a'i suspension or mixturewhich has the ow characteristics -of a fluid.' J This mixture isxdirected through a reaction chamberor zone 29, which-.is shown in the formof a continuousfpipevor, coil. In order to maintain the temperatur-esL of the suspension' -of vapors and catalyst, .the reactor, is

f either heavily insulated or is positioned in 'a furnace setting` to which the desired heat is supplied to maintain proper reaction temperatures. j .The

i discharge end ofthe reactor.l is `connected ,toia

separator-30 wherein the solid particles are separated from thersuspension `andare `drawn off through a bottom 'dischargellnezS l controlled by valve 32. This discharge pipe feeds-into agconveyor arrangement 33, which directs :thefsolid catalyst to the regenerating .or revivifyinggstage. They vaporsfseparated from thecatalystgin the separating vessel `30pass out;through the vapor line 34 and are passed inheat exchange with the charge in exchanger 4,; andare thereafter Aconf densed at 35 andI directed toareceiver A36 through pipe 31. The `receiver.is equippe:l with a liquid draw-olf line 38 and a gas line 39 controlled `by a Valve40.. The conveyor y33, into vwhich is charged cataf lyst from the separator, 30, maybe.r a vdevice of similar design and, ,function -asthat shownI-at 2.3,

Instead, however', "ot' using hydrocarbon vapor, flue gas is used to carry thek catalyst particles through-the regeneration zone.` This gas is obtained fromfany source, such as the gas holder 4i] from which it is withdrawn through line 4i, and pumped by compressor 42 through line 43 control-led by valve 44 to conveyor 33, where it is intimately combined with the catalyst discharged from the separator. The gas catalyst mixture passes through thepipe 45 into the revivier 46, wherein the temperature is controlled within a range ot irom'ODto 1290" F. as a maximum by introducing additional flue gas asv required. To the revivien at a plurality of points along the travel of thegas catalyst mixture therethrough, air is supplied by means of compressor 48 through connecting .lines 49 andi 50, which are equipped with-secondary connections 5l and 52 regulated bysuitable valves. The amount of air or other oxidizing mediumv supplied to the gas catalyst mixture is determined by the temperatures at which the catalyst is revivified and the extent of contamination. From the revivier the mixture passes through pipe 5ty and is discharged into the cyclone separator 21a, where the ycatalyst is permitted to separate from the gas, the gas rising into the top or. .the cyclone and is withdrawn through pipe 54l by means of which it is returned to the nue gas holder40. Valve 55 controls the iiow of gas returned through pipe 54. Excess or make ue gas maybe withdrawn from the systern through pipe 2 l controlled by valve 2da.

Catalyst is withdrawn from the bottoni of cyclone `separator 21a' and discharged into a conveying device 23a which may be. similar in ccnstruction to device 23. Flue gas supplied through by-pass linef43a may be introduced into 23a and utilized to recycle "the regenerated catalyst through line54a to the feedv hopper or cyclone separator 21. rator 21d, line` maybe connected directly to and dischargedinto cyclone separator 21, thereby dispensing with cyclone separator 21a and connecting lines thereto.

Inthe modified type of construction shown in Fig. 2, the ,charge-is fed from any suitable source through line 56 rby means or pump 51 through exchanger 58 to the heating coil 59 positioned in furnace B. After being raised to a vaporizing temperature, the oil vapor mixture is separated in anv evaporatorq l` equipped with a liquid draw-ot.F line 62 and vapor draw-oit line 63. A recirculation line84 is furnished to charge back portions of bottoms into the transfer line between heater 59 and evaporator 6l. f The vapors are superheated in a heater positioned in furnace 6G, and are thence passedthrough line E1 into a Vapor catalyst mixing pump G8, similar in character to that shown at 23 inFig, l. Catalyst is supplied to the pump 58 from a hopper or cyclone separator 59. The catalyst` .vapor mixture is discharged from the pump B8 through line 1B into reactor 1l, the discharge end of the transfer pipe 10 terminating in a nozzle or aspirating arrangement 10a whereby the catalystrvapor mixture is maintained inthe reactor in theform of a cloud, mist or fog 10b during the reaction period. A separate connectiorrlZv between the line 61 and the reaction chamberl furnishes a means for by-passing vapors around the mixing pump and directly to the reaction chamber. A valve in line 12 may be regulated to control the amount of vapors by-passed. Thenozzle arrangement 16a at the discharge end ofthe pipe 10 may be of any suitable type, either a devicewhich.` mechanically whirls the suspen- In place of discharging into sepa- L as to direct the suspension of cloud orxvapor cat- T-fi alyst mixture so that it is uniformly distributed throughout the catalyst chamber. A` baille 10c may be provided in the upper part of the reactor 1l to assist in the maintenance of the desired cloud or mist of catalyst in the reaction Zone. The bottom of the reactor 'tl is inclined to direct catalyst separated from the suspension into a discharge pipe 13 controlled by valve 14 into conveyor 15. From the reactor 1l the vapor catalyst suspension containing the catalyst not separated through valve 14 passes through pipe 1t to sepa.- rator 'il where the solid particles of catalyst are separated from the vapors. The vapors from the separator are directed through the vapor line 18 through exchanger 53 and condenser 19 to the gas separator or receiver 83, which is equipped with a liquid draw-oil* line 8| and a gas line S2. Catalyst removed from the vapors in the separator 11 passes out through pipe S3 controlled by valve S4 to the conveyor 'l5 where it `ioins the catalyst Withdrawn from the bottom of reactor 1l, the combined catalyst passing through line 85 to hop-- per S36 which feeds mixing device 81, similar in character to that shown at B8. The mixing. and` conveying device t? is supplied with iiue gas from the holder td through pipe S9 and ilue gas compressor 9d. This nue gas compressor discharges the flue gas through pipe tl connected to mixer EVE, and also through pipe 82 to a separate mixing device hereinafter described. The flue gas catalyst mixture or suspension formed in mixing device 8i is passed through pipe 93 into a reviviiier 94, oi similar construction to the reactor 1|, the mixture of flue gas and catalyst being discharged in the form of a cloud or mist in the reviviying chamber', there being supplied an oxidizing gas such as air by means of compressors through pipe 55. Valves in the flue gas and air supply lines furnish means for controlling the supply of the respective mediums. Catalyst which separates from the flue gas in the revivifying chamber is Withdrawn through line 91 controlled by valve 98. The revivication product gases pass from the revivier 94 through line 99 to a separator S53, where any remaining catalyst particles are removed rom the gaseous combustion products or nue gas. This catalyst is withdrawn through line itil controlled by valve l t2 and is combined with the catalyst removed from the revivifying chamber in .a conveyor itt, The flue gas is discharged -from the separator it through line itil controlled by valve 8&5, and is returned to the flue gas holder 8&3 through line 88a. Aline H36 controlled by a suitable valve furnishes a means for withdrawing excess or make flue gas from the system. The revivied catalyst picked up by the conveyor m3 is discharged into a hopper lil1 from which it is supplied toa conveying device |98, which be similar to that shown at t3. Flue gas is introduced into this device through line 92 to serve a carrier medium to return the revivified catalyst through pipe Hi@ back to the cyclone separator or hopper attached to the mixing device 68. Hopper i831 and mixing device Hi8 may be dispensed with by discharging catalyst from conveyor H23 directly into hopper G8. When so directly discharged into cyclone 69, it will be apparent that the regenerated catalyst will remain at the high temperature to which it is raised during regeneration and will be at approximately the temperature required for conversion. Dependent upon the temperature of the catalyst thus supplied, the temperature of the oil vapor may be regulated so that the temperature of the combined vapor-catalyst mixture is that desired for the cracking or other conversion reaction involved. Fresh ycatalyst may be supplied to the hopper 69 through pipe I I controlled by suitable valve.

`Figure illustrates an alternative type of device for dispersing the catalyst particles in the reactant vapors, this type of device being employed in what is known commercially as the Airveyor pneumatic conveying system. With this device,

the catalyst is fed from a suitablefsource 2lb through a rotary seal 28h and drops into the oil Vapor which is passed through line 22a at a high velocity. This type of dispersing device lacks a number of advantages of the device illustrated by Figure 3 `as applied to the present process. The latter Vdevice is especially advantageous in that it may be used with a relatively high proportion of catalyst to oil in the feed mixture, and also the compacted catalyst in the catalyst supply conduit provides an effective seal between the various parts of the system. The catalyst employed in the process is prefer-v ably introduced in finely divided or powdered condition, that is, about 20 to'200 mesh material or ner. vThe chemical composition and physical structure of the catalyst selected is dependent upon the type of hydrocarbon conversion involved, and the catalyst employed may be any one of the many available types. For catalytic cracking, known types of cracking catalysts such as activated clays, for example, Super Filtrol, silica gel activated with alumina, and similar types of silica-alumina type of catalysts are preferred;

Reaction conditions such as temperature, pressure, proportions of catalyst and oil in the feed mixture and dimensions of the reactor are determined with respect to the proper conversion of the particular stock treated and quantity thereof charged. A catalyst to oil feed ratio of 3 to 1 by weight is typical of a suitable feed ratio for catalytic cracking, utilizing a cracking catalyst of the type indicated above. Satisfactory operating conditions Afor any particular predetermined requirements such as a particular charging stock, particular catalyst, and extent and degree of conversion, are necessarily determined by several experimental runs as will be apparent to those skilled in the art, and one of the advantages of the process is the extreme flexibility it permits in l conversion zone l I, and then again into a zone of high velocity in the transfer line 16 leading to the separating zone 11. Furnace transfer line velocities in accordance with conventional practice are usually maintained within the range of about to ft./second. In the travel of the dispersion of catalyst and vvapors upwardly through the zone 1I, the effect of "slip in building-up of an increased concentration of the catalyst (compared with the concentration in line 10) is greatly ac- I centuated due to the low vapor velocity in zone Il and produces what mayr be termed a cloud-like formation of catalyst particles in the reactor. Any catalyst particles separating out from the dispersion at the bottom of the reactor due to the low vapor velocities maintained in zone 1| may be withdrawn through valve 15.

In general, it will be noted that the methods of catalytically converting hydrocarbons described in the foregoing exhibits `a number of important distinct features and advantages. One of the features of the process resides in its continuous operation and the circulation of the finely divided catalyst in dispersed condition in both the conversion and regeneration zones. A further feature of the process is the interrelation preferably maintained between the regeneration operation and conversion operation arising from the temperature control of the catalyst between these zones. The process in this respect contemplates as `a preferred condition the transfer of the catalyst from the conversion zone to the regeneration zone at a temperature above its ignition temperature, and the transfer from theregeneration zone to the conversion zone at a temperature approximating the required conversion temperature.

A further feature of the process resides in its extreme flexibility. The use of a conveying and mixing device such as `illustrated in Figure 3 makes it feasible to introduce a dispersion into the system comprising a very high proportion of catalyst relative to the oil introduced.

A further feature of the operation particularly that shown in Figure 2 is the relatively high concentration of catalyst which may be maintained in the reaction and regeneration zones.

It will be understood that certain features and sub-combinations are of utility and may be employed Without reference to other features and sub-combinations. This is contemplated by and is within the scope of the claims.

It is further obvious that various changes may be made in detail within the scope of the claims without departing from the spirit of the invenion.

It is, therefore, to be understood that the invention is not to be limited to the specific details shown and described.

This application is a division of Ser. No. 376,316, filed January 28, 1941, now U. S. Patent No. 2,417,- 973, which is a continuation-in-part of Ser. No.

202,252, filed April 15, 1938, now U. S. Patent No.

yintroducing and dispersing finely divided solid catalyst in the absence of liquid oil directly into said superheated restricted vapor stream in sufficient amount to substantially convert said heated hydrocarbon vapors, the catalyst particles being maintained in motion in the reaction zone by the action of the vapor stream, separating at least partially deactivated catalyst from said converted vapors within said enlarged reaction zone, regenerating said at least partially deactivated catalyst by continuously feeding and dispersing it in a stream of oxygen-containing gas, regulating the regeneration temperature substantially above the temperature to which said vapors are superheated, continually separating said gas from said regenerated catalyst and continually returning 9 the thus separated regenerated'caitalyst and introducing it while still hot and without any .intervening -cooling treatment t0 Asaid superheated hydrocarbon vapor stream.

l V2. vA continuousuprocess. for cracking hydro- ,cazrbon oils involving cyclicallycirculating cata1yst ithrough a hydrocarbon conversion zone in contact with theoil component in the vaporous phasepndycataflyst regeneration zone in contact (with Aanoxyger1-containing gaseomponent which comprises employing said catalyst in a nely divided form having a particle size such that it may be readily picked up by gases in the form of a suspension, contacting the hydrocarbons to be cracked with hot regenerated catalyst, the said hydrocarbons having been preheated to a temperature not higher than 925 F., introducing said hot regenerated catalyst and vapors of said hydrocarbons to be cracked into said conversion zone at a cracking temperature, passing said vapors through said conversion zone, maintaining said regenerated catalyst in motion in said vapors in said conversion zone by the suspending action of said vapors to effect the desired cracking, withdrawing reaction products and spent catalyst from said conversion zone, introducing said Spent catalyst and an oxygen-containing gas into said regeneration zone, passing said oxygen-containing gas through said regeneration zone, maintaining said spent catalyst in motion in said oxygencontaining gas in said regeneration zone by the suspending action of said gas at a temperature eective to revivify said catalyst and substantially higher than the temperature to which said hydrocarbons are preheated prior to contact with said catalyst, withdrawing flue ygas and hot regenerated catalyst from said regeneration zone, and conveying the hot regenerated catalyst without intervening cooling treatment into the conversion zone at a point substantially distant from the point of exit of the reaction products.

3. A continuous process for cracking hydrocarbon oils involving cyclically circulating catalyst through a hydrocarbon conversion zone in contact with the oil component in the vaporous phase and catalyst regeneration zone in contact with an oxygen-containing gas component which comprises employing said catalyst in a finely divided form having a particle size such that it may be readily picked up by gases in the form of a suspension, contacting the hydrocarbons to be cracked with hot regenerated catalyst, the said hydrocarbons having been preheated to a tempera-ture not higher than 925 F., introducing said hot regenerated catalyst and vapors of said hydrocarbons to be cracked into said conversion zone at a cracking temperature, passing said vapors through said conversion zone, maintaining said regenerated catalyst in suspension in said vapors in said conversion zone to effect the desired cracking, withdrawing reaction products and spent catalyst from said conversion zone, introducing said spent catalyst and an oxygen-containing gas into said regeneration zone, passing said oxygen-containing gas through said regeneration zone, maintaining said spent catalyst in suspension in said oxygen-containing gas in said regeneration zone at a temperature effective to revivify said catalyst and substantially higher than the temperature to which said hydrocarbons are preheated prior to contact with said catalyst, withdrawing ilue gas and hot regenerated catalyst from said regeneration zone, and conveying the hot regenerated catalyst without intervening cooling treatment into the conversion zone at a point substantially ydistant from the point of exit of the reaction products.

L4. A continuous process for cracking vhydrocarbon oils involving cyclically circulating catalyst through a hydrocarbon conversion zone in contact with the oil component in the vaporous phase and .catalyst :regeneration zone in contact with an oxygen-containing gas component which comprises employing said catalyst in a finely divided formA having a :particle size such that it may be readily picked up by gases in the vforni of ,-a suspension, contacting the hydrocarbons to be cracked with hot regenerated catalysts, the said hydrocarbons having been preheated to a temperature not higher than 925 F., introducing said hot regenerated catalyst and vapors of said hydrocarbons to be cracked into said conversion zone at a cracking temperature, passing said vapors through said conversion zone, maintaining said regenerated catalyst in suspension in said vapors in said conversion zone to effect the desired cracking, withdrawing reaction products containing a portion of the' catalyst in suspension therein from the reaction zone at an upper point thereof and separately withdrawing the remainder of the catalyst from the reaction zone from the lower portion thereof, introducing said spent catalyst and an oxygen-containing gas into said regeneration zone, passing said oxygen-containing gas through said regeneration zone, maintaining said spent catalyst in suspension in said oxygen-containing gas in said regeneration zone at a temperature eiective to revivify said catalyst and substantially higher than the temperature to which said hydrocarbons are preheated prior to contact with said catalyst, withdrawing iiiie gas and hot regenerated catalyst from said regeneration zone, and conveying the hot regenerated catalyst without intervening cooling treatment into the conversion zone at a point substantially distant from the point of exit of the reaction products.

5. A continuous process for cracking hydrocarbon oils involving cyclically circulating cata1yst through a hydrocarbon conversion zone in contact with the oil component in the vaporous phase and catalyst regeneration zone in contact with an oxygen-containing gas component which comprises employing said catalyst in a finely divided form having a particle size such that it may be readily picked up by gases in the form of a suspension, contacting the hydrocarbons to be cracked with hot regenerated catalyst, the said hydrocarbons having been preheated to a temperature not higher than 925 F., introducing said hot regenerated catalyst and vapors oi said hydrocarbons to be cracked into said conversion zone at a cracking temperature, passing said vapors through said conversion zone, maintaining said regenerated catalyst in suspension in said vapors in said conversion zone to effect the desired cracking, :withdrawing reaction products and spent catalyst from said conversion zone, introducing said spent catalyst and an oxygen-containing gas into said regeneration zone, passing said oxygen-containing gas through said regeneration zone, maintaining said spent catalyst in suspension in said oxygen-containing gas in said regeneration zone at a temperature effective to revivify said catalyst and substantially higher than the temperature to which said hydrocarbons are preheated prior to contact with said catalyst, withdrawing flue gas containing hot regenerated catalyst suspended therein from a high point in the regeneration zone and separately withdraw- A11 1 l2 Y ing additional hot regenerated ''.atalyst from a. UNITED STATES PATENTS low point in the regeneration zone, and convey- Nmber Name Date ing lhot regenerated .catalyst WithO'ui? ntelven- 1934 330` @den Dec, 13 '1934 ingeooling treatment into the conversion zone n 2231231 Subkow Feb 11 1941 at a, point substantially distant from the point f, 2231 424 Huppke w Feb 11 1941 of exit 0f the reaction Products- 2'253466 Belchetz .ffl-..12 Au. 19 1941 WILLIAM J DEGNEN- 2,356,680 Marancik et a1 Aug. 22, 1944 2,384,356 Tyson Sept. 4, 1945 REFERENCES CITED 2,387,798 Kubieek et a1. oct. 3o, 1945 The following references are of record in the W 2,403,375 Kassel July 2, 1946 le of this patent: 

1. IN THE PROCESS OF CONTINUOUSLY CONVERTING HYDROCARBON OILS INTO HIGH KNOCK RATING MOTOR FUELS WHEREIN A HYDROCARBON OIL IS CONTACTED WITH A SOLID CONVERSION CATALYST IN FINELY DIVIDED FROM AT AN ELEVATED TEMPERATURE, THE IMPROVEMENT COMPRISING COMPLETELY VAPORIZING SAID OIL IN A RESTRICTED STEAM AND SUPERHEATING THE VAPOR STREAM TO A TEMPERATURE NOT HIGHER THAN 925*F., THEN CONDUCTING SAID VAPOR STREAM AT HIGH VELOCITY TO AN ENLARGED REACTION ZONE, CONTINUOUSLY INTRODUCING AND DISPERSING FINELY DIVIDED SOLID CATALYST IN THE ABSENCE OF LIQUID OIL DIRECTLY INTO SAID SUPERHEADED RESTRICTED VAPOR STREAM IN SUFFICIENT AMOUNT TO SUBSTANTIALLY CONVERT SAID HEATED HYDROCARBON VAPORS, THE CATALYST PARTICLES BEING MAINTAINED IN MOTION IN THE REACTION ZONE BY THE ACTION OF THE VAPOR STREAM, SEPARATING AT LEAST PARTICALLY DEACTIVATED CATALYST FROM SAID CONVERTED VAPORS WITHIN SAID ENLARGED REACTION ZONE, REGENERATING SAID AT LEAST PARTIALLY DEACTIVATED CATALYST BY CONTINUOUSLY FEEDING AND DISPERSING IT IN A STREAM OF OXYGEN-CONTAINING GAS, REGULATING THE REGENERATION TEMPERATURE SUBSTANTIALLY ABOVE THE TEMPERATURE TO WHICH SAID VAPORS ARE SUPERHEATED, CONTINUALLY SEPARATING SAID GAS FROM SAID REGENERATED CATALYST AND CONTINUALLY RETURNING THE THUS SEPARATED REGENERATED CATALYST AND INTRODUCING IT WHILE STILL HOT AND WITHOUT ANY INTERVENING COOLING TREATMENT TO SAID SUPERHEATED HYDROCARBON VAPOR STREAM. 